WO2008058875A1 - Procédé de préparation d'un catalyseur de fcc - Google Patents

Procédé de préparation d'un catalyseur de fcc Download PDF

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Publication number
WO2008058875A1
WO2008058875A1 PCT/EP2007/061992 EP2007061992W WO2008058875A1 WO 2008058875 A1 WO2008058875 A1 WO 2008058875A1 EP 2007061992 W EP2007061992 W EP 2007061992W WO 2008058875 A1 WO2008058875 A1 WO 2008058875A1
Authority
WO
WIPO (PCT)
Prior art keywords
aluminum chloride
zeolite
poly aluminum
clay
preparation
Prior art date
Application number
PCT/EP2007/061992
Other languages
English (en)
Inventor
Monique Van Der Zon
Jan Hendrik Hilgers
Original Assignee
Albemarle Netherlands B.V.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Albemarle Netherlands B.V. filed Critical Albemarle Netherlands B.V.
Priority to CA2669210A priority Critical patent/CA2669210C/fr
Priority to AT07822306T priority patent/ATE486654T1/de
Priority to JP2009535716A priority patent/JP5185943B2/ja
Priority to EP07822306A priority patent/EP2086675B1/fr
Priority to DE602007010342T priority patent/DE602007010342D1/de
Priority to CN2007800419456A priority patent/CN101563158B/zh
Publication of WO2008058875A1 publication Critical patent/WO2008058875A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/084—Y-type faujasite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0027—Powdering
    • B01J37/0045—Drying a slurry, e.g. spray drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles

Definitions

  • the present invention relates to a process for the preparation of a fluid catalytic cracking (FCC) catalyst by spray-drying an aqueous slurry comprising a zeolite, clay, and poly aluminum chloride.
  • FCC fluid catalytic cracking
  • the compound wherein y 5 is commonly referred to as aluminum chlorohydrol.
  • GB 2 109 696 discloses a process for the preparation of FCC catalyst particles involving spray-drying of an aqueous mixture of an alkali metal-containing zeolite, clay, and aluminum chlorohydrol with an 0H/A1 ratio of 2 to 2.67 and, hence, a y-value in the above-mentioned formula in the range of 4 to 5.14.
  • the resulting particles are subsequently calcined and ion- exchanged.
  • the present invention therefore relates to a process for the preparation of a fluid catalytic cracking catalyst wherein an aqueous slurry comprising a zeolite, clay, and poly aluminum chloride is spray-dried and subsequently calcined, the poly aluminum chloride having the formula [Al2(OH) y Cl6- y ] x , wherein x is at least 1 and y is greater than 2 and smaller than 4. In other words, the OH/ Al ratio in the poly aluminum chloride is greater than 1 and less than 2.
  • the value of y ranges from about 2.2 to about 3.6. In an even more preferred embodiment, the value of y ranges from about 2.4 to about 3.0.
  • a conventional manner of producing poly aluminum chloride is the attack of aluminum metal with hydrogen chloride.
  • Other methods are disclosed in GB 1,376,885 and DE 29 07 671.
  • the first document discloses a process, which involves the attack of aluminum hydroxide particles (gibbsite, boehmite, bayerite) with HCI, followed by electrolysis.
  • the current that is used during the electrolysis determines the CI/A1 ratio and, hence, the 0H/A1 ratio of the resulting poly aluminum chloride.
  • the aqueous slurry that is used in the process according to the invention comprises zeolite, clay, and poly aluminum chloride.
  • the zeolite is preferably selected from the group of faujasite zeolites (e.g. zeolite X and Y), ZSM-5, phosphorus-exchanged ZSM-5, zeolite beta, MCM-22, MCM-36, ITQ-zeolite, SAPO, ALPO, and mixtures thereof. More preferred are Y-type zeolites such as zeolite Y, ultrastable zeolite Y (USY), rare earth exchanged (ultrastable) zeolite Y (RE-Y and RE- US Y), and mixtures of these Y-type zeolites with ZSM-5.
  • zeolite Y ultrastable zeolite Y (USY), rare earth exchanged (ultrastable) zeolite Y (RE-Y and RE- US Y
  • RE-Y and RE- US Y rare earth exchanged zeolite Y
  • Suitable clays include kaolin, bentonite, English clay, and heat- or chemically treated clays such as meta-kaolin.
  • the clay preferably has a low sodium content, typically below about 0.1 wt% Na 2 O.
  • alumina e.g. (pseudo)boehmite, gibbsite, heat-treated forms of gibbsite such as flash-calcined gibbsite
  • silica e.g. silica sol, sodium silicate, sodium-free silica, (poly)silicic acid
  • anionic clays e.g. hydrotalcite
  • saponite e.g. montmorillonite
  • highly crystalline alumina e.g.
  • a specifically preferred additional compound is alumina.
  • the slurry preferably comprises about 5 to about 30 wt%, more preferably about 7 to about 20 wt%, and most preferably about 8 to about 12 wt% of poly aluminum chloride, calculated as AI2O3 and based on the total solids content of the slurry.
  • the slurry preferably comprises: about 10 to about 70 wt%, more preferably about 15 to about 50 wt%, and most preferably about 15 to about 40 wt% of zeolite, about 5 to about 70 wt%, more preferably about 10 to about 60 wt%, and most preferably about 10 to about 50 wt% of clay, and about 1 to about 50 wt%, more preferably about 2 to about 40 wt%, and most preferably about 3 to about 40 wt% of alumina, calculated as AI2O3. These weight ranges are all based on the solids content of the slurry.
  • the solids content of the slurry preferably is about 10 to about 60 wt%, more preferably about 20 to about 50 wt%, and most preferably about 30 to about 46 wt%.
  • the slurry is prepared by adding the clay, zeolite, and poly aluminum chloride, and optional other components (such as alumina) to water.
  • the clay, zeolite, and other components can be added as dry solids or in aqueous suspension.
  • Poly aluminum chloride is added as sol or solution. Any order of addition may be used.
  • the pH of the slurry to be spray-dried preferably is above about 3, more preferably in the range of about 3 to about 5.5, and most preferably in the range of about 3.5 to about 4.5.
  • the slurry is spray-dried to form fluidizable particles, i.e. particles with a size in the range of about 10 to about 200 microns, preferably about 20 to about 150 microns.
  • the inlet temperature of the spray-dryer preferably ranges from about 300 to about 600 0 C and the outlet temperature preferably ranges from about 105 to about 200 0 C.
  • the catalysts are calcined.
  • the calcination temperature preferably is in the range of about 120 to about 700 0 C, more preferably in the range of about 400 to about 600 0 C. Calcination is preferably performed from about 5 minutes to about 3 hours, more preferably about 10 to about 60 minutes.
  • the resulting FCC catalyst has a high attrition resistance. If so desired, the FCC catalyst may be further treated by ion-exchange procedures, before its use in an FCC process.
  • catalyst compositions were prepared by mixing 30 wt% of zeolite Y, 50 wt% of kaolin clay, 10 wt% of alumina, and 10 wt% of poly aluminum chloride with water at 35% solids. All weight percentages are based on dry solids content
  • the catalysts 10 differed In the 0H/A1 ratio (and, hence, in the y-value in the formula [Al2(OH) y Cl6- y ] x ,) of the poly aluminum chloride that was used for their preparation.
  • These different poly aluminum chlorides were purchased from Gulbrandsen Chemicals.
  • the attrition resistance of the catalysts was measured by the standard Attrition Test.
  • the catalyst bed resides on an attrition plate with three nozzles.
  • the attrition plate is situated within an attrition tube, which is at ambient temperature. Air is forced to the nozzles and the resulting jets bring about upward transport of catalyst particles and generated fines.
  • On top of the attrition tube is a separation chamber where the flow dissipates, and most particles larger than about 16 microns fall back into the attrition tube. Smaller particles are collected in a collection bag.
  • catalyst compositions were prepared by mixing 30 wt% of zeolite Y, 50 wt% of kaolin clay, 10 wt% of alumina, and 10 wt% of poly aluminum chloride with water at 35% solids. All weight percentages are based on dry solids content.
  • the catalysts differed in the OH/Al ratio of the poly aluminum chloride that was used for their preparation.
  • the different poly aluminum chlorides were prepared by boiling mixtures of aluminum metal and HCl in Al/Cl ratios that correspond to the desired OH/Al ratios, according to the formula [Al 2 (OH) y Cl6- y ] x .
  • the attrition resistance of the catalysts was measured by the Attrition Test outlined in Example 1.
  • the attrition indices of the different catalysts are listed in Table 2.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un procédé de préparation d'un catalyseur de craquage catalytique fluide présentant une résistance à l'attrition améliorée. Selon ce procédé de préparation, une suspension aqueuse comprenant une zéolite, de l'argile, et du chlorure de poly aluminium est séchée par pulvérisation puis calcinée, le chlorure de poly aluminium ayant la formule [Al2(OH)yCl6-y]x, dans laquelle x est au moins 1 et y est supérieur à 2 et inférieur à 4.
PCT/EP2007/061992 2006-11-13 2007-11-07 Procédé de préparation d'un catalyseur de fcc WO2008058875A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
CA2669210A CA2669210C (fr) 2006-11-13 2007-11-07 Procede de preparation d'un catalyseur de fcc
AT07822306T ATE486654T1 (de) 2006-11-13 2007-11-07 Verfahren zur herstellung eines fcc-katalysators
JP2009535716A JP5185943B2 (ja) 2006-11-13 2007-11-07 Ｆｃｃ触媒の製造方法
EP07822306A EP2086675B1 (fr) 2006-11-13 2007-11-07 Procédé de préparation d'un catalyseur de fcc
DE602007010342T DE602007010342D1 (de) 2006-11-13 2007-11-07 Verfahren zur herstellung eines fcc-katalysators
CN2007800419456A CN101563158B (zh) 2006-11-13 2007-11-07 一种fcc催化剂的制备方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US85836506P 2006-11-13 2006-11-13
US60/858,365 2006-11-13

Publications (1)

Publication Number Publication Date
WO2008058875A1 true WO2008058875A1 (fr) 2008-05-22

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2007/061992 WO2008058875A1 (fr) 2006-11-13 2007-11-07 Procédé de préparation d'un catalyseur de fcc

Country Status (8)

Country Link
US (1) US7442664B2 (fr)
EP (1) EP2086675B1 (fr)
JP (1) JP5185943B2 (fr)
CN (1) CN101563158B (fr)
AT (1) ATE486654T1 (fr)
CA (1) CA2669210C (fr)
DE (1) DE602007010342D1 (fr)
WO (1) WO2008058875A1 (fr)

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JP5258488B2 (ja) * 2008-09-30 2013-08-07 日揮触媒化成株式会社 炭化水素の流動接触分解触媒
WO2011115785A1 (fr) 2010-03-18 2011-09-22 W. R. Grace & Co.-Conn. Compositions catalyseur de craquage catalytique en lit fluide (fcc) pour une haute production d'oléfines légères
WO2011115746A1 (fr) 2010-03-18 2011-09-22 W. R. Grace & Co.-Conn. Procédé de fabrication de catalyseurs améliorés à partir de zéolites dérivées de l'argile
BR112012023069B1 (pt) 2010-03-18 2018-11-21 W.R. Grace & Co - Conn. processo para fabricar um catalisador e método de reduzir a perda da área da superfície do zeólito em um catalisador contendo zeólito
US9518229B2 (en) * 2012-07-20 2016-12-13 Inaeris Technologies, Llc Catalysts for thermo-catalytic conversion of biomass, and methods of making and using
JP5579236B2 (ja) * 2012-09-18 2014-08-27 日揮触媒化成株式会社 炭化水素の流動接触分解触媒の製造方法
RU2500472C1 (ru) * 2012-12-24 2013-12-10 Миррико Холдинг ЛТД Способ получения гранулированного катализатора крекинга
US9522392B2 (en) 2013-03-15 2016-12-20 Inaeris Technologies, Llc Phosphorous promotion of zeolite-containing catalysts
CN103611579B (zh) * 2013-11-19 2016-04-13 神华集团有限责任公司 改进沉淀铁费托催化剂前体料浆特性的方法、料浆及制法、由料浆制备的催化剂及制法
EP3609616A4 (fr) * 2017-04-14 2020-12-09 BASF Corporation Catalyseur de craquage catalytique fluide à faible teneur en coke et rendement élevé en essence et à haute activité
CN107138175A (zh) * 2017-05-15 2017-09-08 江苏有容催化技术研究所有限公司 一种高活性高选择性甲醇制丙烯催化剂的制备方法
CN109701597B (zh) * 2017-10-26 2022-07-12 中国石油化工股份有限公司 高水热稳定性的甲醇制芳烃催化剂及其用途
CN109701598B (zh) * 2017-10-26 2022-04-05 中国石油化工股份有限公司 甲醇制芳烃催化剂及其用途
CN109701599B (zh) * 2017-10-26 2022-07-08 中国石油化工股份有限公司 甲醇制芳烃的催化剂及其用途方法
CN109701622B (zh) * 2017-10-26 2022-07-12 中国石油化工股份有限公司 甲醇制芳烃的流化床催化剂
JP7481439B2 (ja) 2019-10-29 2024-05-10 ダブリュー・アール・グレース・アンド・カンパニー－コーン 修飾ゼオライト触媒組成物及び使用方法

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GB2109696A (en) * 1981-08-10 1983-06-08 Grace W R & Co Method for preparing a zeolite- containing fluid cracking catalyst
US4443553A (en) * 1982-09-20 1984-04-17 Harshaw/Filtrol Partnership Production of fluid catalytic cracking catalysts
US4987110A (en) * 1987-05-07 1991-01-22 Union Oil Company Of California Attrition resistant cracking catalyst
US4837396A (en) * 1987-12-11 1989-06-06 Mobil Oil Corporation Zeolite beta containing hydrocarbon conversion catalyst of stability
US5173463A (en) * 1988-09-06 1992-12-22 Petroleo Brasileiro, S.A.-Petrobras Kaolin containing fluid cracking catalyst

Also Published As

Publication number Publication date
CA2669210C (fr) 2015-05-26
DE602007010342D1 (de) 2010-12-16
EP2086675B1 (fr) 2010-11-03
US7442664B2 (en) 2008-10-28
EP2086675A1 (fr) 2009-08-12
JP2010509044A (ja) 2010-03-25
CN101563158A (zh) 2009-10-21
CA2669210A1 (fr) 2008-05-22
CN101563158B (zh) 2011-11-09
ATE486654T1 (de) 2010-11-15
US20080146436A1 (en) 2008-06-19
JP5185943B2 (ja) 2013-04-17

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